Process to recover ammonium bicarbonate from wastewater

ABSTRACT

The present invention is a process, a method, and system for recovery and concentration of dissolved ammonium bicarbonate from a wastewater containing ammonia (NH3) using gas separation, condensation, and crystallization, each at controlled operating temperatures. The present invention includes 1) removal of ammonia from waste (sludges, semi-solids, and solids and liquids) without the use of chemicals at a temperature of at least 80 degrees Celsius, 2) condensing the gaseous containing ammonia, carbon dioxide and water vapor to remove water vapor concentrating the amount of gaseous ammonia and carbon dioxide, 3) concentrating the ammonia and carbon dioxide in the water by established means, such as concentrating the gas using partial condensation followed by passing the concentrated gas through an absorption column at a temperature of between about 20 and 50 degrees Celsius to form dissolved ammonium carbonate and ammonium bicarbonate, or total condensation followed by dewatering using reverse osmosis, and 4) crystallizing concentrated dissolved ammonium carbonate and ammonium bicarbonate at a temperature of less than about 35 degrees Celsius to form solid ammonium bicarbonate and ammonium carbonate.

CROSS-REFERENCE TO RELATED APPLICATION

This application in a continuation in part of, and claims the benefitof, U.S. application Ser. No. 14/852,836 filed on Sep. 14, 2015, whichclaims the benefit of U.S. Application Ser. No. 62/103,191 filed on Jan.14, 2015, and U.S. Application Ser. No. 62/133,549 filed on Mar. 16,2015, each which is expressly incorporated herein in its entirety byreference thereto.

FIELD OF THE INVENTION

The present invention relates generally to a process, a method, and asystem for the recovery and concentration of dissolved ammoniumbicarbonate from a wastewater containing ammonia (NH3) using gasseparation, condensation, and filtration, each at controlled operatingtemperatures. The present Invention also relates generally to a process,a method, and a system for the recovery and concentration of dissolvedammonium bicarbonate from a wastewater containing ammonia (NH3) usinggas separation, condensation, and crystallization, each at controlledoperating temperatures. Wastewaters may contain dissolved ammonia asammonium ion and as dissolved ammonia gas; as well as dissolved carbondioxide as bicarbonate and carbonate ions and as dissolved carbondioxide gas. The word “ammonia” will be used generally to refer to anydissolved form of ammonia. The present invention also relates to aprocess, a method, and a system for the production of a nitrogen richfertilizer from an ammonia (NH3) containing wastewater using a process,method and/or system comprising the concentration of dissolved ammoniumbicarbonate using gas separation and condensation, followed bycrystallization of concentrated ammonium bicarbonate, all at controlledoperating temperatures. More specifically, the present invention relatesto a process, method, and system to produce, from a wastewatercontaining ammonia (NH3), an organic solid containing highconcentrations of nitrogen which could be utilized as a componentingredient in a nitrogen rich, organic fertilizer product. The process,method and system of the present invention is a useful improvement overexisting technologies for the removal of ammonia from wastewatersbecause the present invention: converts NH3-N into ammonia gas but doesnot utilize any chemicals to increase pH, captures the ammonia gas inthe form of a stable salt but does not utilize industrial acids to reactwith the ammonia, and produces a solid-fertilizer product with minimaluse of energy.

The present invention allows for the production/synthesis of organicN-fertilizer, ammonium bicarbonate (AB) derived from wastewaters,sludges and solids containing ammonia (NH3) or ammonia and carbondioxide (CO2), without the use of chemical additives.

BACKGROUND OF THE INVENTION

Anaerobic digestion is a common unit operation employed in the treatmentof wastewaters containing organics and nitrogenous compounds includingindustrial, municipal and agricultural wastewaters. The resultingsolid/liquid slurry from an anaerobic digester has a high-solids portionand a low-solids portion. For example, the digestate produced from dairywastewater, contains a high-solids portion comprising largely cellulosicsolids and a low-solids portion containing concentrations of dissolvedcarbon dioxide and dissolved ammonia nitrogen as well as salts and bothsuspended and dissolved organics. The dissolved ammonia nitrogen in thedigestate presents significant environmental issues if left untreated,such as, when the digestate is land applied, discharged to a body ofwater, or sent to a holding pond or lagoon. Potential adverse air andwater impacts include: ammonia (toxic to fish, irritating to human eyesand lungs) will be lost both to the air and water; ammonia will bebiologically oxidized either in water or soil and chemically oxidized inthe air, in either case forming gases that are irritants and can formozone or greenhouse gases, etc. Most often regulations for ammoniarelease are designed to prevent excess nutrient input to surface waterswhich may cause eutrophication.

Effective treatment technologies are needed for agricultural andindustrial waste streams that may release ammonia to the environment.For example, anaerobic digester digestate is often high in ammonia andtheir sources are required to remove ammonia nitrogen to avoid excessivenitrogen discharges.

One well-established technology for treatment of digestate is airstripping which uses hot air and/or steam to strip ammonia from thewastewater creating a liquid stream comprising substantially lessdissolved ammonia and a heated gas containing the stripped ammonia.Formation of a solid precipitate containing ammonia, ammoniumbicarbonate, and ammonium carbonate, during the air stripping processmay foul the air stripping substrates causing operational andmaintenance issues and thus is not desired. An increase of the pH of thewastewater shifts the equilibrium for ammonia away from dissolvedionized ammonium and more to ammonia gas. Accordingly, increased removalof the ammonia from digestate using air stripping is commonly achievedwith chemical addition. Examples of chemicals used to increase pHinclude calcium, sodium or magnesium hydroxide. The stripped ammonia isabsorbed into an acid solution. The use of acids is highly effective forammonia recovery and could also be effective in producing a concentratedammonium salt product using subsequent unit operations. On the otherhand, treatment utilizing industrial chemicals to raise pH with astripping process and for absorption of ammonia, such as, for example,for a treatment system for a dairy waste which produces a nutrient richsolid for use as a fertilizer, has the unavoidable consequence stemmingfrom the use of such chemicals that any reusable end product cannot becertified as an “organic” product.

Stripper exhaust gas containing ammonia is sometimes released to theatmosphere although regulations typically require that it is furtherprocessed to capture the nitrogen. For example, U.S. Pat. No. 7,811,455(Burke) describes a process for use of biogas rather than air andreclaiming ammonia from stripper exhaust gases in the form of ammoniumbicarbonate by blending the CO2 in the digester biogas with the strippergas and then precipitating and recovering ammonium bicarbonate with theadded benefit of lowering CO2 in the biogas. One of the main drawbackswith that process is that the use of chemicals to raise the pH in thestripper precludes certification of the ammonium bicarbonate solids andany solids created from the ammonium bicarbonate solids as “organic”fertilizer. Another drawback is the inefficiency associated withprocessing large volumes of gas, including precipitation of ammoniumbicarbonate in the gas phase.

There is a need for a waste treatment technology that convertswastewater containing nutrients into beneficial use materials that canbe certified as organic. There is a need for a wastewater treatmenttechnology that can remove dissolved ammonia nitrogen, react theresulting gaseous ammonia with carbon dioxide to re-form dissolvedammonium bicarbonate, concentrate the dissolved ammonium bicarbonate,and then capture the ammonium bicarbonate in crystalline form. There isa need for an improved manure treatment system comprising anaerobicdigestion that does not utilize expensive, hazardous, chemicals to raisethe pH of digestate, chemicals that present significant handling andstorage issues. There is a need for an improved wastewater treatmentsystem that effectively removes and recovers nitrogen in the form ofammonium bicarbonate without any chemical addition.

SUMMARY OF THE INVENTION

Applicants have invented a new process, system, and method for treatingwastewater that satisfies these needs. While the invention will bedescribed in connection with certain embodiments, it will be understoodthat the invention is not limited to those embodiments. To the contrary,the invention includes all alternatives, modifications and equivalentsas may be included within the spirit and scope of the present invention.

High-ammonia and ammonium containing wastewaters are produced in manyindustrial and municipal processes. Agriculture is one of the largestsources of these wastewaters, in particular in the form of products fromthe anaerobic digestion of organic waste. Examples of sources of thiswaste are animal manure, meat processing, dairy processing, and silage.Ammonia (NH3) that is not captured in a stable chemical form is apotential source of air and water pollution.

The present invention provides a way to remove a substantial portion ofthe ammonia nitrogen within a liquid wastewater and capture the nitrogenin the form of crystallized ammonium bicarbonate using a series of unitoperations operated under specified temperatures and without the use ofchemicals to raise pH. The resulting ammonium bicarbonate solid is highin nitrogen content and could be used in combination with othermaterials to create a nitrogen rich organic fertilizer product.

In one embodiment, the present invention includes at least threecomponents:

-   -   1) removal of the ammonia from the waste (including without        limitation sludges, semi-solids, and solids and liquids) without        the use of chemicals at a temperature of at least 80 degrees        Celsius thereby converting the ammonia to gaseous form;    -   2) mixing of the gaseous ammonia with carbon dioxide and water        vapor at a temperature of between about 20 and 50 degrees        Celsius causing the formation of dissolved ammonium carbonate        and ammonium bicarbonate in a liquid condensate and        concentrating the dissolved ammonium carbonate and ammonium        bicarbonate using reverse osmosis also operating at a        temperature of between about 20 and 50 degrees Celsius; and    -   3) crystallizing the concentrated dissolved ammonium carbonate        and ammonium bicarbonate at a temperature below 35 degrees        Celsius such that the reverse osmosis concentrate becomes        saturated with dissolved ammonium bicarbonate and ammonium        carbonate which depends upon the concentrations of ammonium        carbonate and ammonium bicarbonate to form solid ammonium        bicarbonate and ammonium carbonate.

In a second embodiment using partial condensation of digester gases toeliminate the need for a filter (reverse osmosis), the present inventionincludes at least three components:

-   -   1) removal of the ammonia from the waste (including without        limitation sludges, semi-solids, and solids and liquids) without        the use of chemicals at a temperature of at least 80 degrees        Celsius thereby converting the ammonia to gaseous form;    -   2) staged condensation and concentration of the gas containing        gaseous ammonia, carbon dioxide, and water vapor, at a        temperature at least 80 degrees Celsius to remove a significant        amount of water vapor in liquid condensate form causing        formation of a concentrated gas, followed by the formation of a        concentrated dissolved ammonium bicarbonate liquid solution        using absorption operating at a temperature of between about 20        and 50 degrees Celsius; and    -   3) crystallizing the concentrated dissolved ammonium carbonate        and ammonium bicarbonate at a temperature below 35 degrees        Celsius such that the concentrated dissolved ammonium carbonate        and ammonium bicarbonate becomes saturated with dissolved        ammonium bicarbonate and ammonium carbonate which depends upon        the concentrations of ammonium carbonate and ammonium        bicarbonate to form solid ammonium bicarbonate and ammonium        carbonate.

The present invention is not limited to any one specific method orprocess to remove ammonia nitrogen from the waste but rather includesnumerous alternatives provided the operating temperatures for thecomponents are followed. Stripping animal manure digestate at atemperature of at least 60 degrees Celsius and preferably at atemperature of at least 80 degrees Celsius, for example, is one way toremove ammonia nitrogen from animal waste creating an exhaust gascontaining ammonia gas. Examples of other ways to remove ammonianitrogen from wastewaters and create an ammonia-containing gas includedryers, and filtration devices with membrane modules and heat sources.

Once the dissolved ammonia is removed from the waste and is in gaseousform, the present invention includes two paths for the creation of aconcentrated solution of ammonium carbonate and ammonium bicarbonate,the first using condensation to convert gaseous ammonia, CO2 and watervapor to a liquid solution containing ammonium carbonate and ammoniumbicarbonate followed by filtration, the second using staged condensationto remove a significant amount of water vapor from the gas by partialcondensation causing formation of a concentrated gas, followed by theformation of a concentrated dissolved ammonium bicarbonate liquidsolution using absorption of ammonia from said gas. The presentinvention then uses crystallization to form solid ammonium bicarbonateand ammonium carbonate.

When using condensation and reverse osmosis, the present inventionincludes condensing the gaseous ammonia with carbon dioxide and watervapor at a temperature of between about 35 and 50 degrees Celsiuscausing the formation of dissolved ammonium carbonate and ammoniumbicarbonate in a liquid condensate. Depending upon the characteristicsof the waste and the preceding treatment processes, the amount of carbondioxide within the ammonia-containing gas may be enough to convertsubstantially all of the ammonia into ammonium carbonate and ammoniumbicarbonate without addition of carbon dioxide. Digested dairy manure,for example, put through a stripping process operated at greater than 80degrees Celsius should create an exhaust gas containing enough carbondioxide for the conversion of substantially all of the gaseous ammoniato dissolved ammonium carbonate and ammonium bicarbonate. The net resultof the process is to recover ammonium bicarbonate and ammonium carbonatefrom the mixture of materials constituting the digestate as a highpurity solution of ammonium bicarbonate and ammonium carbonate in thecondensate. The formation of the ammonium carbonate and ammoniumbicarbonate without the use of chemicals in the ammonia removal step,and without an outside source for carbon dioxide permits organiccertification of the eventually created nitrogen rich solids. Ifadditional carbon dioxide is required, the organic certification canstill be used if the carbon dioxide is from non-synthetic sources. Whileorganic fertilizers have a significant financial advantage overnon-organic fertilizers, the present invention is not limited solely toa process, method, or system resulting in organic products. The presentinvention also includes addition of carbon dioxide from outside sourcesresulting in products unable to be certified as organic.

The dissolved ammonium carbonate and ammonium bicarbonate in theresulting condensate liquid is then concentrated. A two-stage reverseosmosis unit operating between about 20 and 50 degrees Celsius, forexample concentrates dissolved ammonium carbonate and ammoniumbicarbonate to about 10 times the ammonium concentration of thecondensate, but the increase could be anywhere from 1.5 to 20 times theconcentration of the ammonium concentration in the condensate. Morepreferably, a two-stage reverse osmosis unit operating between about 35and 50 degrees Celsius, concentrates dissolved ammonium carbonate andammonium bicarbonate more efficiently.

When using condensation and absorption, the present invention includescondensing the gaseous ammonia is a staged manner at a temperature of atleast 80 degrees Celsius in the first stage to remove a significantamount of water vapor in liquid condensate form causing formation of aconcentrated ammonia and carbon dioxide gas. Removing the water vaporand concentrating the ammonia and carbon dioxide gas at this pointinstead of condensing the gas with all the water vapor eliminates theneed to concentrate the ammonium bicarbonate solution after condensationusing filters. It may eliminate the need, cost, and maintenance expenseof a filtering unit process, potentially providing a more efficient andcost effective overall process. The concentrated ammonia and carbondioxide gas is then treated using absorption (an absorption column, forexample) operating at a temperature of between about 20 and 50 degreesCelsius to form a concentrated dissolved ammonium bicarbonate liquidsolution.

The liquid containing concentrated dissolved ammonium carbonate andammonium bicarbonate is then cooled to less than about 35 degreesCelsius to saturate the reverse osmosis or absorption concentrate andform solid ammonium bicarbonate and ammonium carbonate which is stableand high in nitrogen content. Moreover, resulting solids aresubstantially free of phosphorous. The solid ammonium bicarbonate can bestored and/or combined with other materials to create nitrogen richfertilizer.

Although the detailed chemistry for the formation of ammoniumbicarbonate from ammonia and carbon dioxide is complex, the reactionsprovide predictable behaviors at temperatures and pressures accessibleunder normal industrial and agricultural conditions. At biological pHabout 8, ammonium bicarbonate is stable in solutions below about 50degrees Celsius and rapidly decomposes in solutions above about 80degrees Celsius, as displayed in Table 2 below. The present inventionutilizes the varying stability and solubility of ammonium bicarbonate atdifferent temperatures and pressures a) to drive substantially all ofthe dissolved ammonium out of the wastewater and into gaseous form(which occurs at a temperature of about 80 degrees Celsius (Table 2) andis complete at a temperature of about 90 degrees Celsius (Table 1)), b)so that it can be condensed with carbon dioxide and water vapor andconcentrated at a lower temperature (at a temperature of between about35 and 50 degrees Celsius) where ammonium bicarbonate is stable, therebyconverting the ammonia to dissolved ammonium bicarbonate in aconcentrated liquid form, and c) so that the concentrated dissolvedammonium bicarbonate can be solidified at a lower temperate (less thanabout 20 degrees Celsius).

The following table shows how the solubility (and stability) of ammoniumbicarbonate varies with temperature. Weast, R. C. (ed.) Handbook ofChemistry and Physics. 69th ed. Boca Raton, Fla.: CRC Press Inc.,1988-1989; Perry's Chemical Engineers' Handbook, 6th Edition, McGrawHill, 1997.

TABLE 1 Variation of solubility of different substances (mostlyinorganic compounds) in water with temperature, under 1 atmospherepressure. Units of solubility are given in grams per 100 grams of water(g/100 g) Temperature (Degrees C.) Range Substance Formula 10 15 20 3040 50 60 70 80 90 100 Ammonium NH₄HCO₃ 16.1 21.7 28.4 36.6 59.2 109 decbicarbonate Ammonium (NH₄)₂CO₃•H₂O 10 dec carbonate Ammonium NH4NO3 150192 242 297 344 421 499 580 740 871 nitrate Ammonium (NH4)2SO4 73 75.478.1 81.2 84.3 87.4 94.1 103 sulfate dec = decomposition of compound atspecified temperature

TABLE 2 Fraction of ammonia-N in the form of ammonia gas at conditionsof pH and temperature. T F\ f = 1/(1 + 10{circumflex over ( )}(pKa-pH))T K T C pKa pH 7 8 9 10 11 300 27 9.20 80 0.01 0.06 0.39 0.86 0.98 32249 8.57 120 0.03 0.21 0.73 0.96 1.00 333 60 8.29 140 0.05 0.34 0.84 0.981.00 344 71 8.02 160 0.09 0.49 0.90 0.99 1.00 355 82 7.78 180 0.14 0.630.94 0.99 1.00 pKa from National Research Council. Ammonia. UniversityPark Press, Baltimore, MD (1979).

BRIEF DESCRIPTION OF THE DRAWINGS

The accompanying drawings, which are incorporated in and constitute apart of this specification, illustrate embodiments of the invention and,together with the general description of the invention given above andthe detailed description of an embodiment given below, serve to explainthe principles of the present invention. Similar components of thedevices are similarly numbered for simplicity.

FIG. 1 is a schematic drawing of one embodiment of the invention for thetreatment of cattle manure (e.g., from a CAFO) comprising solidsseparation, anaerobic digestion, stripping, condensation, concentrationusing reverse osmosis, and crystallization.

FIG. 2 is a schematic drawing of another embodiment of the invention forthe treatment of dairy manure (e.g., from a CAFO) comprising solidsseparation, anaerobic digestion, ultra filtration with heating andmembrane filtration, condensation, concentration using reverse osmosis,crystallization, and storage.

FIG. 3 is a schematic drawing of another embodiment of the invention forthe treatment of an ammonia-containing wastewater (e.g., from layermanure) comprising heat drying, condensation of ammonia water,dissolution of carbon dioxide into the ammonia water using membranefilters, concentration of ammonium bicarbonate, crystallization, andstorage.

FIG. 4 is a schematic drawing of another embodiment of the invention forthe treatment of cattle manure (e.g., from a CAFO) comprising solidsseparation, anaerobic digestion, stripping, absorption, concentrationusing reverse osmosis, and crystallization. The carbon dioxide dissolvedin solution within the anaerobic digester's digestate, which derivesdirectly from the cattle manure waste, is supplemented by carbon dioxideremoved from the biogas.

FIG. 5 is a schematic drawing of another embodiment of the invention forthe treatment of livestock manure (e.g., from a CAFO) comprising solidsseparation, anaerobic digestion, stripping, condensation, absorption,and crystallization. The carbon dioxide dissolved in solution within theanaerobic digester's digestate, which derives directly from thelivestock manure waste, may be supplemented by carbon dioxide removedfrom the biogas.

DETAILED DESCRIPTION OF THE INVENTION

The accompanying drawings, which are incorporated in and constitute apart of this specification, illustrate embodiments of the invention and,together with the general description of the invention given above andthe detailed description of an embodiment given below, serve to explainthe principles of the present invention. Similar components of thedevices are similarly numbered for simplicity.

FIG. 1 is a process flow schematic drawing of one embodiment of theinvention for the treatment of cattle manure (e.g., from a CAFO)comprising solids separation, anaerobic digestion, stripping,condensation, concentration, and crystallization. In the processaccording to FIG. 1, there is no chemical addition to adjust pH priorto, or in, the stripping process. The present invention excludes the useof pH adjustment chemicals. In the process according to FIG. 1, there isalso no external supply of carbon dioxide. The carbon dioxide dissolvedin solution within the anaerobic digester's digestate, which derivesdirectly from the cattle manure waste, is the sole source for carbondioxide in the process.

As depicted in FIG. 1, raw manure 10 with or without associated dairywaste generated at the CAFO is transported to a solids separationunit/process 20 (it being understood that a mixing or holdingtank/vessel could be used prior to solids separation and/or can be usedfor solids separation). The solids separation unit/process may be asingle stage or chamber unit or it could be a series of stages orchambers for coarse solids separation and intermediate solidsseparation.

The slurry/effluent 24 from the solids separation unit 20 is input intoan anaerobic digester 30 which digests much, preferably most, of thedissolved organics and small organic particulates to produce biogas 32and an effluent digestate 34.

The effluent digestate 34 from the anaerobic digester 30 containsresidual solids, dissolved salts and organics, and concentrations ofdissolved ammonia and carbon dioxide. The present invention collects theammonia and carbon dioxide and captures them in a subsequent multistageprocess to re-form solid ammonium bicarbonate. Each stage of thesubsequent multistage process operates at different temperatures to takeadvantage of the solubility properties of ammonium bicarbonate for itsconcentration in dissolved form and then its formation as a nitrogenrich solid.

The temperature of digestate 34 out of a typical anaerobic digestertreating cattle manure is about 35 degrees Celsius. For the process ofthe invention, the digestate needs to be heated to greater than about 80degrees Celsius for treatment in the stripper 40.

The stripper operating at a temperature of greater than about 80 degreesCelsius, without any chemical addition to increase pH, removes dissolvedammonia and dissolved carbon dioxide from the digestate 34 creatingexhaust vapor 42 containing water vapor, gaseous carbon dioxide, andgaseous ammonia. Vapor 42 will also contain traces of organic volatilesand semi-volatiles. In FIG. 1, footnote 1 denotes the vapor is constantcomposition for continuous operation and varies during a batchprocess—H2O, CO2, and NH3 evolve with traces of organic volatiles andsemi volatiles. The treated water and solids 44 out of the stripper canbe further treated for application to land or water using currenttreatment technologies. The temperature of the stripper 40 can bemaintained using a heat exchanger 46. The vapor 42 created by strippingthe digestate 34 in that first stage, the separation stage, is thentreated in a second condensation and concentration stage to create aconcentrated dissolved ammonium bicarbonate solution.

Condenser 50 and reverse osmosis filter 60 are then used to treat vapor42 at a temperature of between about 35 degrees Celsius and 50 degreesCelsius. A pressure control valve 48 can be used between the stripper 40and the condenser 50 to maintain a differential between the two. In FIG.1, footnote 2 denotes pressure control valve is set to maintaindifferential between distillation unit and condenser—Condensertemperature, T, must be less than 50 degrees Celsius to keep NH4 andHCO3 in solution, while distillation temperature must be greater than 80degrees Celsius to convert to NH3 and CO2. Operating the condenser 50between about 35 and 50 degrees Celsius allows the water vapor, ammonia,and carbon dioxide to form dissolved ammonium bicarbonate. Maintainingbetween about 35 and 50 degrees Celsius in the condenser 50, and a pHless than 9, prevents precipitation of dissolved ammonium bicarbonate orammonium carbonate and keeps it in dissolved form. The temperature ofthe condenser 50 can be maintained using a heat exchanger 56. Thenon-condensed water and gases 52 exiting the condenser 50 can bedischarged to the atmosphere. In FIG. 1, footnote 3 denotes AB solutionin condenser is distillate of feed to stripping device.

Following the condenser 50, and operating at about the same temperatureas the condenser 50, the effluent ammonium bicarbonate solution 54 istreated in a reverse osmosis filter 60. Reverse osmosis filter 60removes water thereby concentrating the ammonium bicarbonate in thesolution. The resulting concentrated effluent 64 out of the reverseosmosis filter 60 contains about 50-100 times the concentration ofdissolved ammonium bicarbonate in the digestate 34. In FIG. 1, footnote5 denotes AB concentrate is supersaturated relative to temperature ofcrystallizer. Control of the reverse osmosis temperature avoidsprecipitation of the ammonium bicarbonate on the membrane whileachieving a concentration sufficient for saturation at the temperaturein the crystallizer. The permeate 62 is a clean water than can be reusedor discharged.

The concentrated effluent 64 out of the reverse osmosis filter 60 isthen treated at a temperature of less than about 35 degrees Celsius instage three using a crystallizer 70. It is understood that lowertemperatures, e.g., 20 degrees Celsius, could be used in thecrystallizer depending upon the concentrations of dissolved ammoniumcarbonate and ammonium bicarbonate in the reverse osmosis concentrate.Solid crystals of ammonium bicarbonate are grown in the crystallizer 70under controlled conditions, separated from the liquid fraction toproduce an ammonium-salt 74 which may be dried, pelletized or granulatedto form a final product. In some embodiments, a portion of the saturatedammonium bicarbonate supernatant is recycled 72 to the reverse osmosisfilter 60, after it is heated to the required temperature in a heatexchanger 56. In FIG. 1, footnote 4 denotes heat exchange onrecirculation liquid to minimize size of heat exchanger 56 to matchtemperature of reactor liquid.

Due to the unique sequence of the preceding unit operations, theresulting ammonium salt may be dried and packaged for commercialdistribution as a specialized nitrogen fertilizer, that is high-purity,phosphorus free, and certified USDA organic. The resulting product ishigh-purity and phosphorous free due to the two purification operations,namely, 1) the distillation process which removes ammonia and separatesit from salts that are left behind in the distillation unit's liquideffluent, and 2) the crystallization process which removes solidammonium bicarbonate from other contaminants including traces ofphosphorous containing salts. If synthetic chemicals are not used inobtaining the solids or liquid digestate, the ammonium bicarbonateproduct will have the potential for designation as organic (USDA 2012)fertilizer. The USDA designation is of economic importance as the priceof organic fertilizer expressed as dollars per pound ammonia nitrogen,is materially higher than that of chemical (non-organic) fertilizersthat are equally uniform, high purity, and concentrated sources ofNH3-N. As with synthetic fertilizer, the material is nearly odorless,and has low transport and application costs relative to manure anddigestate. If the ammonia is captured with an industrial acid or isderived from application of caustic or other industrial alkali—it willnot qualify as organic fertilizer. The ammonium salt according to theinvention resolves this conflict by (1) producing ammonia gas thermallywith no chemical addition, and (2) using the carbon dioxide found in thedigestate to recover the ammonia from the digestate to form an organicfertilizer, ammonium bicarbonate.

The ammonium salt 74 can be stored 80 for use on or off site.

Another embodiment of the invention for a wastewater that utilizessolids reduction prior to membrane separation of ammonia is shown inFIG. 2. In such instances, stage 1 of the foregoing described processcan be modified to remove solids (effluent suspended solids of 0.1% orless) so that a membrane separation device could be employed to separatethe gases water vapor, carbon dioxide, and ammonia from the digestateliquid.

As depicted in FIG. 2, raw manure 110 with or without associated dairywaste generated at the CAFO is transported to a solids separationunit/process 120 (it being understood that a mixing or holdingtank/vessel could be used prior to solids separation or for theseparation). The solids separation unit/process 120 may be a singlestage or chamber unit or it could be a series of stages or chambers. InFIG. 2, the footnotes 1-4 denote the following:

-   -   [1]—mesophilic digester, 35 C        -   digested dairy manure, typical ammonia nitrogen is 1000 ppm        -   AB is ammonium bicarbonate. Calculated from NH3-N and MW            ratio        -   AB concentration is 1% of saturation at 35 C        -   digested manure is high in TSS        -   No pH adjustment by either chemical addition or CO2 removal    -   [2]—gas from Separation Device has 20× concentration of ammonia        as input        -   NH3-N is 60% NH3 at 80 C, 34% NH3 at 60 C, and 4% NH3 at 20        -   Temperature must be about 80 C or higher to convert NH4+ to            NH3        -   AB concentration is about 5% of saturation at 80 C        -   Nearly all the TSS is removed by the uF    -   [3]—Condensate <50 C to convert dissolved NH3 and CO2 to        dissolved AB, and >35 C to avoid precipitation in lines or RO        -   AB concentrate from RO is about 81% of saturation at 50 C        -   pH must be less than 9 to avoid carbonate formation and            precipitation        -   Recycle of liquor from crystallizer to RO has about the same            concentration as the RO concentrate, and must be heated to            the RO temperature    -   [4] Solids from crystallizer are high-purity, certifiable        organic N-fertilizer

The output/effluent from the solids separation unit 124 is input into ananaerobic digester 130 which digests much, preferably most, of thedissolved organics and small organic particulates to produce biogas 132and an effluent digestate 134.

The temperature of digestate 134, about 35 degrees Celsius, is heated togreater than about 80 degrees Celsius for treatment in stage 1, asdescribed in detail below. Here again, as for the previous embodiment,the invention excludes the addition of chemicals to increase pH and alsoexcludes the addition of carbon dioxide from a non-organic source(preferably, the carbon dioxide used in the process comes directly fromthe waste being treated). For the embodiment shown in FIG. 2, an inputvapor similar to that created in the foregoing embodiment shown in FIG.1 containing water vapor, gaseous carbon dioxide, and gaseous ammonia,is created using a different unit process than shown in FIG. 1. In FIG.2, the separation of the gaseous ammonia and gaseous carbon dioxide fromthe digestate 134 is accomplished using a membrane device 143 instead ofa stripper. The membrane passes gases, such as water vapor, ammonia, andcarbon dioxide, but not liquid water. It therefore performs the samegas-separation function as the separation device shown in stage 1 ofFIG. 1.

As shown in FIG. 2, the digestate 134 is treated for solids removalprior to stage 1, the ultrafilter 136, and prior to gas separation inthe membrane device 143. An ultra filter 136 is shown in FIG. 2 for thesolids removal it being understood that other solids removal methodsproducing the equivalent result of fine solids removal, for examplepassing only solids of less than 0.5 micron, are included within thescope of the invention. The concentrated solids 138 from the ultrafilter 136 can be mixed with the solids from the initial solidsseparation step, or processed as a high phosphorus solid product. Theultra filter 136 removes a substantial portion of the total suspendedsolids in the digestate. The low suspended-solids (0.1% or less)digestate 137 is then treated in the gas-separation process of theinvention which in this embodiment includes use of membrane device 143.The temperature of the low-solids digestate 137 is raised to at leastabout 80 degrees Celsius using a heat exchanger 146. Membrane device 143includes a hydrophobic membrane that allows gas molecules to pass, suchas water vapor, ammonia, and carbon dioxide, but not the liquid and itscontaminants. The preceding uF is required to remove solids and organicmaterial that might otherwise foul the hydrophobic membrane. Vapor 142will also contain traces of organic volatiles and semi-volatiles. Thetreated water and solids 149 out of the membrane device 143 can befurther treated for application to land or water using current treatmenttechnologies.

The vapor 142 created from the digestate using the membrane device 143in that first stage, the separation stage, is then treated in stage 2and stage 3 using condensation and concentration, respectively, followedby crystallization, similar to the embodiment shown in FIG. 1.

Condenser 150 and reverse osmosis filter 160 are used to condense vapor142 and concentrate its condensate 154 at a temperature of between about35 and 50 degrees Celsius, to hold stable ammonium bicarbonate insolution. The effluent ammonium bicarbonate solution 154 out of thecondenser 150 contains the dissolved ammonium bicarbonate from theammonia and carbon dioxide of the digestate 134. The non-condensed waterand gases 152 exiting the condenser 150 can be discharged to theatmosphere.

Following the condenser 150, and operating at about the same temperatureas the condenser 150, the effluent ammonium bicarbonate solution 154 istreated in a reverse osmosis filter 160. Reverse osmosis filter 160removes water thereby concentrating the ammonium bicarbonate in thesolution. The resulting concentrated effluent 164 out of the reverseosmosis filter 160 contains about 10 times the concentration ofdissolved ammonium bicarbonate in the condenser effluent 154. Thepermeate 162 is a clean water than can be reused or discharged.

The concentrated effluent 164 out of the reverse osmosis filter 160 isthen treated at a temperature of less than about 35 degrees Celsius,preferably less than 20 degrees Celsius, in stage 3 using a crystallizer170. Solid crystals of ammonium bicarbonate are grown in thecrystallizer 170 under controlled conditions, separated from the liquidfraction to produce an ammonium-salt 174 which may be dried, pelletizedor granulated to form a final product. In some embodiments, a portion ofthe saturated ammonium bicarbonate supernatant is recycled 172 to thereverse osmosis filter 160.

A resulting ammonium salt 174 solid, having physical and chemicalproperties as stated above for the first embodiment will result. Theammonium salt can be stored 180 for use on or off site.

Yet another embodiment of the invention using an external source forcarbon dioxide is shown in FIG. 3. Such an embodiment could be used forwastes that do not contain the carbon dioxide needed to convert theammonia to ammonium bicarbonate. Examples of such wastes include wastenot processed using anaerobic digestion, such as high-solids manure orother organic waste. In the embodiment shown in FIG. 3, as compared tothe embodiment shown in FIG. 1, stage 1 and stage 2 are modified. InFIG. 3, stage 1 comprises a dryer 247 in place of a stripper and stage 2includes the addition of membrane modules 253 with a source of carbondioxide 255 along with a condenser 250 and a reverse osmosis filter 260.In FIG. 3, the footnotes 1-4 denote the following:

[1]—dryer exhaust to 2-stage condenser

-   -   ammonia water at 2× exhaust ammonia concentration, temperature        between 20 and 35 C

[2]—ammonia stabilized with CO2 as acid

-   -   P adjusted to provide CO2 to stabilize ammonia water in effluent    -   CO2 flow rate equals CO2 as HCO3 in effluent liquid.

[3]—Ammonium bicarbonate at 20 C in cystallizer

-   -   Mother liquor recycled to RO, and must be heated to the RO        temperature

[4]—inject compressed vent gas (CO2, H2O, NH3) into ammonia water feedline. Here again, as for the previous embodiments, the inventionexcludes the addition of chemicals to increase pH. For the embodimentshown in FIG. 3, a solution of ammonium bicarbonate is created andcrystallized as in the foregoing embodiments shown in FIGS. 1 and 2. InFIG. 3, the separation of the gaseous ammonia from the waste 234 isperformed using a dryer 247, an ammonia water is created usingcondensers 250, and gaseous carbon dioxide is contacted with the ammoniawater solution using membrane device 253 to create a solution ofammonium bicarbonate.

As depicted in FIG. 3, the waste (such as layer manure) 234 is treatedin stage 1 of the process of the invention which in this embodimentincludes use of dryer 247. The temperature of the dryer is at leastabout 80 degrees Celsius. Dryer 247 operates at a sufficiently hightemperature that the ammonia in the waste is converted to gas andremoved with the water vapor. The dryer functions as a separation devicein a manner analogous to the distillation process 40 in FIG. 1. Theexhaust vapor 242 from the dryer 247 contains water vapor and gaseousammonia and lower than desired concentrations of carbon dioxide. In thisembodiment, it is assumed that there is an insufficient amount of carbondioxide in the waste to react with and convert substantially all of thegaseous ammonia into dissolved ammonium bicarbonate and thus, additionalcarbon dioxide is required. The dried waste 244 out of the dryer 247 canbe processed further into solid products such as fertilizer, animal feedsupplement, or fuel.

The vapor 242 created using the dryer 247 in stage 1, the separationstage, is then treated in stage 2 using condensation, carbon dioxideaddition, and concentration.

FIG. 3 shows an example of a two-step condenser 250 to create an ammoniawater 258 from the dryer exhaust gas 242. The first step removes aboutone half of the water and nearly no ammonia (NH3) and the second step iscomplete condensation producing ammonia water at about 50 degreesCelsius or less. The concentration of the dissolved ammonia in thecondensate will be about twice that in the dryer vapor, for exampleabout 0.5% by weight. The non-condensed water and gases 252 exiting thecondenser 250 can be discharged to the atmosphere.

The ammonia water 258 is then treated in a membrane device 253 where anexternal source of gaseous carbon dioxide 255 is added. The gaseouscarbon dioxide passes through the membrane, dissolves into the ammoniawater, and reacts to create a solution of ammonium bicarbonate 254. Forexample, the solution of ammonium bicarbonate may be 2.3% by weightammonium bicarbonate at about pH 6.5-8.5, depending on the amount of CO2added and the temperature.

The ammonium bicarbonate 254 is then treated in a reverse osmosis filter260. Reverse osmosis filter 260 removes water thereby concentrating theammonium bicarbonate in the solution. The resulting concentratedeffluent 264 out of the reverse osmosis filter 260 contains about 20times the concentration of ammonia in the dryer gas. The permeate 262 isa clean water than can be reused or discharged. Stage 2 which includesthe condenser 250, the membrane device 253 and the reverse osmosisfilter 260 operate at a temperature of between about 35 degrees Celsiusand 50 degrees Celsius.

The dissolved ammonium bicarbonate solution 264 is then treated in stage3 using crystallization, similar to the embodiments shown in FIGS. 1 and2. The concentrated effluent 264 out of the reverse osmosis filter 260is cooled to a temperature of less than about 35 degrees Celsius instage 3 using a crystallizer 270. Solid crystals of ammonium bicarbonateare grown in the crystallizer 270 under controlled conditions, separatedfrom the liquid fraction to produce an ammonium-salt 274 which may bedried (such as using dryer 285), pelletized or granulated to form afinal product.

A resulting ammonium salt solid having physical and chemical propertiesas stated above for the first and second embodiments will result.However, the certification as an organic product is contingent upon useof carbon dioxide produced organically. If synthetic carbon dioxide isused, the ammonium bicarbonate product cannot be designated as anorganic fertilizer.

Carbon dioxide produced by fermentation of either animal waste oragricultural material (for example to produce ethanol) is certifiablyorganic; and is readily available from agricultural sources to assurethat the carbon dioxide is neither synthetic nor contaminated withsynthetic carbon dioxide.

FIG. 4 is a process flow schematic drawing of a variation on theembodiment of the invention shown in FIG. 1 for the treatment of cattlemanure (e.g., from a CAFO) comprising solids separation, anaerobicdigestion, stripping, absorption, concentration, and crystallization. Inthe process according to FIG. 4, there is no chemical addition to adjustpH prior to, or in, the stripping process. The present inventionexcludes the use of pH adjustment chemicals. In the process according toFIG. 4, there is also no external supply of carbon dioxide. The carbondioxide dissolved in solution within the anaerobic digester's digestate,which derives directly from the cattle manure waste, is supplemented bycarbon dioxide from the biogas to assure maintenance of CO2 in the waterto stabilize the ammonia in the absorber column. FIG. 4 shows the biogas32 processed in a CO2 removal device 35 to provide CO2 to providecarbonated water for capture of ammonia as ammonium bicarbonate. Forexample, the device could be a pressure swing adsorption device which iscommonly used to separate gases, such as CH4 and CO2, with materiallydifferent properties. In FIG. 4, footnotes 1-5 denote the following:

-   -   [1]—vapor is constant composition for continuous operation and        varies during a batch process. H2O, CO2, and NH3 evolve with        traces of organic volatiles and semi-volatiles.    -   [2]—pressure control valve is set to maintain differential        between stripper unit and absorber. Absorber temperature, T,        must be less than 50 C to keep NH4 and HCO3 in solution, while        stripper temperature must be greater than 80 C to convert to NH3        and CO2.    -   [3]—AB solution in absorber is formed from Digester biogas    -   [4]—HX on recycled stripper gas to match temperature of stripper        liquid.    -   [5]—AB concentrate is supersaturated relative to temperature of        crystallizer.

As depicted in FIG. 4, raw manure 10 with or without associated dairywaste generated at the CAFO is transported to a solids separationunit/process 20 (it being understood that a mixing or holdingtank/vessel could be used prior to solids separation and/or can be usedfor solids separation). The solids separation unit/process may be asingle stage or chamber unit or it could be a series of stages orchambers for coarse solids separation and intermediate solidsseparation.

The slurry/effluent 24 from the solids separation unit 20 is input intoan anaerobic digester 30 which digests much, preferably most, of thedissolved organics and small organic particulates to produce biogas 32and an effluent digestate 34.

The effluent digestate 34 from the anaerobic digester 30 containsresidual solids, dissolved salts and organics, and concentrations ofdissolved ammonia and carbon dioxide. The present invention collects theammonia and carbon dioxide and captures them in a subsequent multistageprocess to form solid ammonium bicarbonate. Each stage of the subsequentmultistage process operates at different temperatures to take advantageof the solubility properties of ammonium bicarbonate for itsconcentration in dissolved form and then its formation as a nitrogenrich solid.

The temperature of digestate 34 out of a typical anaerobic digestertreating cattle manure is about 35 degrees Celsius. For the process ofthe invention, the digestate needs to be heated to greater than about 80degrees Celsius for treatment in the stripper 40.

The stripper operating at a temperature of greater than about 80 degreesCelsius, without any chemical addition to increase pH, uses gas (biogas,CH4, CO2, air, etc) to remove dissolved ammonia and dissolved carbondioxide from the digestate 34 creating exhaust vapor 42 containing watervapor, gaseous carbon dioxide, and gaseous ammonia. Vapor 42 will alsocontain traces of organic volatiles and semi-volatiles. The treatedwater and solids 44 out of the stripper can be further treated forapplication to land or water using current treatment technologies. Thetemperature of the stripper 40 can be maintained using a heat exchanger46 to heat the recycled stripper gas 45 from the absorber. The vapor 42created by stripping the digestate 34 in that first stage, theseparation stage, is then treated with a cold water stream 53 saturatedwith CO2, in an absorption stage 50 to create a dissolved ammoniumbicarbonate solution. Ammonia is removed from the vapor distillate,producing recycled stripper gas 45 which is heated in heat exchanger 46prior to entry at the bottom of stripper 40.

Absorber 50 and reverse osmosis filter 60 are used to treat vapor 42 ata temperature of between about 35 degrees Celsius and 50 degreesCelsius. A pressure control valve 48 can be used between the stripper 40and the absorber 50 to maintain a differential between the two.Operating the absorber 50 between about 35 and 50 degrees Celsius allowsthe water vapor, ammonia, and carbon dioxide to form dissolved ammoniumbicarbonate. Maintaining between about 35 and 50 degrees Celsius in theabsorber 50, and a pH less than 9, prevents precipitation of dissolvedammonium bicarbonate or ammonium carbonate and keeps it in dissolvedform. Temperature of the absorber 50 can be maintained by control of theflow and temperature of the cold water 53.

Following the absorber 50, and operating at about the same temperatureas the absorber 50, the effluent ammonium bicarbonate solution 54 istreated in a reverse osmosis filter 60. Reverse osmosis filter 60removes water thereby concentrating the ammonium bicarbonate in thesolution. The resulting concentrated effluent 64 out of the reverseosmosis filter 60 contains about 50-100 times the concentration ofdissolved ammonium bicarbonate in the digestate 34. Control of thereverse osmosis temperature is critical to avoid precipitation of theammonium bicarbonate on the membrane while achieving a concentrationsufficient for saturation at the temperature in the crystallizer. Thepermeate 62 is a clean water than can be reused or discharged.

The concentrated effluent 64 out of the reverse osmosis filter 60 isthen treated at a temperature of less than about 20 degrees Celsius instage three using a crystallizer 70. Solid crystals of ammoniumbicarbonate are grown in the crystallizer 70 under controlledconditions, separated from the liquid fraction to produce anammonium-salt 74 which may be dried, pelletized or granulated to form afinal product. In some embodiments, a portion of the saturated ammoniumbicarbonate supernatant is recycled 72 to the reverse osmosis filter 60,after it is heated to the required temperature in heat exchanger 56.

Due to the unique sequence of the preceding unit operations, theresulting ammonium salt may be dried and packaged for commercialdistribution as a specialized nitrogen fertilizer, that is high-purity,phosphorus free, and certified USDA organic. The ammonia recovery stepis the equivalent of distillation. This allows nearly no salt (includingphosphorus salts) carry over to the input to reverse osmosis.Crystallization is another purification step, so that “high-purity,phosphorus free” product is achieved. If synthetic chemicals are notused in obtaining the solid AB or liquid digestate, the ammoniumbicarbonate product will have the potential for designation as organic(USDA 2012) fertilizer. The USDA designation is of economic importanceas the price of organic fertilizer expressed as dollars per poundammonia nitrogen, is materially higher than that of chemical(non-organic) fertilizers that are equally uniform, high purity, andconcentrated sources of NH3-N. As with synthetic fertilizer, thematerial is nearly odorless, and has low transport and application costsrelative to manure and digestate. If the ammonia is captured with anindustrial acid or is derived from application of caustic or otherindustrial alkali—it will not qualify as organic fertilizer. Theammonium salt according to the invention resolves this conflict by (1)producing ammonia gas thermally with no chemical addition, and (2) usingthe carbon dioxide found in the digestate to recover the ammonia fromthe digestate to form an organic fertilizer, ammonium bicarbonate.

The ammonium salt 74 can be stored 80 for use on or off site.

FIG. 5 is a process flow schematic drawing of a variation on theembodiment of the invention shown in FIG. 1 for the treatment oflivestock manure (e.g., from a Controlled Animal Feeding Operation,CAFO) comprising solids separation, physical influent conditioning,anaerobic digestion, stripping, condensation (concentration),absorption, and crystallization. In the FIG. 5 process, there is nochemical addition to adjust pH prior to, or in, the stripping process.The present invention excludes the use of pH adjustment chemicals. Inthe process according to FIG. 5, there is also no external supply ofcarbon dioxide. The carbon dioxide, which derives directly from thelivestock manure waste, is supplemented by carbon dioxide from thebiogas to assure maintenance of CO2 in the water to stabilize theammonia in the absorber column. FIG. 5 shows the biogas 32 processed ina CO2 removal device 35 to provide CO2 to for capture of ammonia asammonium bicarbonate. For example, the device could be a pressure swingadsorption device which is commonly used to separate gases, such as CH4and CO2, with materially different properties. In FIG. 5, footnotes 1-4denote the following:

-   -   [1]—vapor is constant composition for continuous operation and        varies during a batch process. H2O, CO2, and NH3 evolve with        traces of organic volatiles and semi-volatiles.    -   [2]—pressure control valve(s) is set to maintain differentials        between a) the stripper unit and the condenser, and b) the        condenser and the absorber. Absorber temperature, T, must be        less than 50 C to keep NH4 and HCO3 in solution, while stripper        temperature must be greater than 80 C to convert to NH3 and CO2.    -   [3]—AB solution in absorber is formed from Digester biogas    -   [4]—AB concentrate is supersaturated relative to temperature of        crystallizer.

As depicted in FIG. 5, raw livestock manure 10 is transported to asolids separation and physical conditioning unit/process 20 (it beingunderstood that a mixing or holding tank/vessel could be used prior tosolids separation and/or can be used for solids separation). The solidsseparation unit/process may be a single stage or chamber unit or itcould be a series of stages or chambers for coarse solids separation,intermediate solids separation, and physical mixing and conditioning.Physical conditioning may include dilution, grinding, mixing, heatingetc., depending on the specific livestock manure processed; dilution maybe necessary for some manure to provide the appropriate consistency andconcentration for the AD, grinding and mixing may be needed to helpsolubilize and make more available the organic content for digestion,heating may be needed for the anaerobic digester influent but may alsobe used to sterilize and prevent biological competition duringdigestion.

The slurry/effluent 24 from the solids separation unit 20 is input intoan anaerobic digester 30 which digests much, preferably most, of thedissolved organics and small organic particulates to produce biogas 32and an effluent digestate 34.

The effluent digestate 34 from the anaerobic digester 30 containsresidual solids, dissolved salts and organics, and concentrations ofdissolved ammonia and carbon dioxide. The present invention collects theammonia and carbon dioxide and captures them in a subsequent multistageprocess to form solid ammonium bicarbonate. Each stage of the subsequentmultistage process operates at different temperatures to take advantageof the solubility properties of ammonium bicarbonate for itsconcentration in dissolved form and then its formation as a nitrogenrich solid.

The temperature of digestate 34 out of a typical anaerobic digestertreating livestock manure is about 35 degrees Celsius. For the processof the invention, the digestate needs to be heated to greater than about80 degrees Celsius for treatment in the stripper 40.

The stripper operating at a temperature of greater than about 80 degreesCelsius, without any chemical addition to increase pH, creates exhaustvapor 42 containing water vapor, gaseous carbon dioxide, and gaseousammonia. Vapor 42 will also contain traces of organic volatiles andsemi-volatiles. The treated water and solids 44 out of the stripper canbe further treated for application to land or water using currenttreatment technologies. The water vapor 42 created by stripping thedigestate 34 in that first stage, the separation stage, is thencondensed in the condenser. The condenser is operated as a single ormultistage unit to condense the water vapor at a high temperature, toseparate water from the gaseous ammonia and CO2 effectivelyconcentrating them in the gas. The amount of ammonium carbonate andammonium bicarbonate concentration in the concentrated gas is at least 2times greater than in the gas before treatment with condensation andcould be as high as 100 times to 1000 times higher. The high temperaturecondensed water 55 is removed from the condenser and may be channeledback to the stripper to reclaim any re-dissolved ammonia and carbondioxide, may be discharged from the process, may be used as seed liquidin the absorber, or may be recycled to combine with the fresh livestockmanure entering the digester.

Absorber 50 is used to treat vapor 142 at a temperature of between about20 degrees Celsius and 50 degrees Celsius. Pressure control valves 48can be used between the stripper 40, the condenser, and the absorber 50to maintain proper differential pressure between the unit processes.Operating the absorber 50 between about 20 and 50 degrees Celsius allowsthe water vapor, ammonia, and carbon dioxide to form dissolved ammoniumbicarbonate. Maintaining between about 20 and 50 degrees Celsius in theabsorber 50, and a pH less than 9, prevents precipitation of dissolvedammonium bicarbonate or ammonium carbonate and keeps it in dissolvedform. Temperature of the absorber 50 can be controlled with a heatexchanger 56 and by regulating the temperature of the carbon dioxide.Since a majority of the water is condensed and removed from the vaporphase prior to the absorber, the amount of water used to generate theconcentrated AB solution is minimized and controlled. The ammonia andcarbon dioxide gasses continue to absorb and form an AB solution in thecontrolled volume of water until they reach close to saturation at theselected temperature between 20 and 50 degrees Celsius.

The concentrated effluent 64 out of the absorber is then treated at atemperature of less than about 20 degrees Celsius in stage four using acrystallizer 70. Solid crystals of ammonium bicarbonate are grown in thecrystallizer 70 under controlled conditions, separated from the liquidfraction to produce an ammonium-salt 74 which may be dried, pelletizedor granulated to form a final product. The more dilute AB solution,following this crystallization process, is returned to the absorber asseed liquid to dissolve more ammonia and carbon dioxide as AB under thehigher temperature conditions, between 20 and 50 degrees Celsius.

The embodiment of the invention shown in FIG. 5 may increase the overallefficiency by potentially eliminating the need for any otherconcentrating unit process, specifically the RO, instead performing theconcentration through removal of water vapor. Substantial reductions incapital cost, energy costs, operating costs, and maintenance costs couldall be realized with that embodiment of the invention. The potential forproduct losses may also be reduced by eliminating or reducing thereverse osmosis, especially since reverse osmosis operates at relativelyhigh pressures. A safer process may also created by eliminating orreducing the high pressure reverse osmosis, it being understood that thepresent invention also includes variations with the addition of areverse osmosis step.

The embodiment of the invention shown in FIG. 5 may eliminate the needfor any other concentrating unit process, specifically the RO, insteadperforming the concentration through removal of water vapor in thepartial condenser and capturing the dissolved AB in the absorber.Substantial reductions in capital cost, energy costs, operating costs,and maintenance costs may be realized with that embodiment of theinvention. While the present invention has been illustrated bydescription of various embodiments and while those embodiments have beendescribed in considerable detail, it is not the intention of applicantto restrict or in any way limit the scope of the appended claims to suchdetails. Additional advantages and modifications will readily appear tothose skilled in the art. The invention in its broader aspects istherefore not limited to the specific details and illustrative examplesshown and described. Accordingly, departures may be made from suchdetails without departing from the spirit or scope of applicants'invention.

We claim:
 1. A process to treat livestock waste containing ammonianitrogen comprising: treating livestock waste at a temperature of atleast 80 degrees Celsius to create a gas and, without the use ofchemicals, converting substantially all ammonia in the waste to gaseousform in the gas, said gas also containing carbon dioxide and watervapor; treating said gas containing gaseous ammonia, carbon dioxide, andwater vapor, using partial condensation to concentrate the ammonia andcarbon dioxide followed by absorption of the concentrate gases, or totalcondensation of said gas followed by dewatering using Reverse Osmosis,or a combination of these methods; all without the use of chemical(s)and remove from said gas a significant amount of water vapor in liquidcondensate form, causing formation of a concentrated gas containinghigher concentrations of ammonia gas and carbon dioxide gas than beforecondensation; treating said concentrated gas using absorption to form adissolved ammonium carbonate and ammonium bicarbonate liquid solution atthe saturation concentrations for dissolved ammonium carbonate andammonium bicarbonate; crystallizing the dissolved ammonium carbonate andammonium bicarbonate condensate liquid solution at a temperature of lessthan about 35 degrees Celsius to form solid ammonium bicarbonate andammonium carbonate.
 2. The process according to claim 1, wherein saidtreating livestock waste at a temperature of at least 80 degrees Celsiuscomprises stripping the waste of ammonia.
 3. The process according toclaim 1, wherein said treating livestock waste at a temperature of atleast 80 degrees Celsius comprises stripping the waste using biogas froman anaerobic digester used to treat the waste prior to stripping.
 4. Theprocess according to claim 1, wherein said treating livestock waste at atemperature of at least 80 degrees Celsius comprises drying the wasteusing a dryer and removing ammonia with the water vapor in gaseous form.5. The process according to claim 1, wherein said treating livestockwaste at a temperature of at least 80 degrees Celsius comprisesseparation of the ammonia and other gases using membrane modules.
 6. Theprocess according to claim 1, wherein substantially all the gaseousammonia in the gas is converted into ammonium carbonate and ammoniumbicarbonate using the carbon dioxide in the gas without the addition ofcarbon dioxide not present in the digestate.
 7. The process according toclaim 6, wherein the waste is a digested dairy manure.
 8. The processaccording to claim 1, wherein substantially all the gaseous ammonia inthe gas is converted into ammonium carbonate and ammonium bicarbonateusing the carbon dioxide in the gas with the addition of carbon dioxidefrom another source.
 9. The process according to claim 1, wherein saidcondensation is a two stage condensation process comprising sequentialcondensation at two temperatures or residence times.
 10. The processaccording to claim 9, wherein said total ammonia and carbon dioxideconcentration in the concentrated gas is at least 2 times greater thanin the gas before treatment with condensation.
 11. The process accordingto claim 1, wherein said dissolved ammonium carbonate and ammoniumbicarbonate concentration in said liquid solution after absorptioncomprises at least about 5 times the concentration of dissolved ammoniumbicarbonate in the digestate.
 12. The process according to claim 1,wherein solid crystals of ammonium bicarbonate grown in the crystallizerare produced creating a solid ammonium-salt.
 13. The process accordingto claim 12, wherein the ammonium-salt is dried, pelletized orgranulated.
 14. A process to treat livestock waste containing ammonianitrogen comprising: treating livestock waste using anaerobic digestioncreating a biogas and a digestate; treating said biogas to separate andconcentrate carbon dioxide in said biogas from other gases in saidbiogas forming a concentrated carbon dioxide biogas; treating saiddigestate at a temperature of at least 80 degrees Celsius to create agas and, without the use of chemicals, converting substantially allammonia in the waste to gaseous form in the gas, said gas alsocontaining carbon dioxide and water vapor; treating said gas fromdigestion containing gaseous ammonia, carbon dioxide, and water vapor,using partial condensation operating at a temperature of at least 80degrees Celsius, without the use of chemicals, to remove from said gas asignificant amount of water vapor and organics in liquid condensateform, causing formation of a condenser effluent concentrated gascontaining higher concentrations of ammonia gas and carbon dioxide gasthan before condensation; treating said concentrated carbon dioxidebiogas and said condenser effluent concentrated gas using absorptionoperating at a temperature of between about 20 and 50 degrees Celsius toform a dissolved ammonium carbonate and ammonium bicarbonate liquidsolution at the saturation concentrations for dissolved ammoniumcarbonate and ammonium bicarbonate at the crystallizer temperature;crystallizing the dissolved ammonium carbonate and ammonium bicarbonatecondensate liquid solution at a temperature of less than about 35degrees Celsius to form solid ammonium bicarbonate and ammoniumcarbonate.
 15. The process according to claim 14, further comprisingrecycling a portion of said saturated dissolved ammonium carbonate andammonium bicarbonate liquid solution from said crystallization to saidabsorber to assist with said absorption.
 16. The process according toclaim 15, wherein substantially all the ammonia in the gas fromdigestion is converted into ammonium carbonate and ammonium bicarbonateusing the carbon dioxide in the livestock waste without the addition ofcarbon dioxide from another source.
 17. The process according to claim14, wherein said treating livestock waste at a temperature of at least80 degrees Celsius comprises stripping the waste of ammonia.
 18. Theprocess according to claim 14, wherein said treating livestock waste ata temperature of at least 80 degrees Celsius comprises stripping thewaste using biogas from an anaerobic digester used to treat the wasteprior to stripping.
 19. The process according to claim 14, wherein saidtreating livestock waste at a temperature of at least 80 degrees Celsiuscomprises drying the waste using a dryer and removing ammonia with thewater vapor in gaseous form.
 20. The process according to claim 14,wherein solid crystals of ammonium bicarbonate grown in the crystallizerare produced creating a solid ammonium-salt.
 21. The process accordingto claim 20, wherein the ammonium-salt is dried, pelletized orgranulated.